Carbon black manufacture



G. L. HELLER ETAL CARBON BLACK MANUFACTURE July 24, 1962 5 Sheets-Sheet 2 Filed Dec. 2, 1958 INVENTORS GEORG I.. HELLER AM OS C. WARNER BY CHARLES L. DeLAND Fun/m1 July 24, 1962 G. l.. HELLER ETAL 3,046,096

CARBON BLACK MANUFACTURE Filed Dec. 2, 1958 5 Sheets-Sheet 3 FIG. 3

INVENTORS GEORGE L. HELLER AMOS C. WARNER g1g CHARLES L. DeLAND July 24, 1962 G. HELLER ETAL CARBON BLACK MANUFACTURE 5 Sheets-Sheet 4 Filed DSO. 2, i958 INVENTORS GEORGE L. HELLER AMOS C. WARNER CHARLES L. DELAND Mlm-u' Wand' f A ORNEYS July 24, 1962 G. HELLER ETAL CARBON BLACK MANUFACTURE 5 Sheets-Siwa?l 5 Filed Dec. 2, 1958 m .GE

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:raisers Patented July 24, 1962 3,046,096 CARBN BLAQK MNUFACTURE George L Heller and Amos C. Warner, Monroe, and

Charles L. De Land, West Monroe, La., assignors to Columbian Carbon Comp-any, New York, N.Y., a corporation of Deiaware Fiied Dec. 2, i958, Ser. No. 777,635 l@ Claims. (Cl. 2li-299.4)

The present invention relates to the production of carbon black by the decomposition of hydrocarbons and, more particularly, to processes of the type whereby the hydrocarbon to be decomposed is separately and forcefully injected into a stream of hot blast tiame gases and rapidly mixed therewith, whereby the hydrocarbon is decomposed by heat absorbed from the hot gases to form carbon black in gaseous suspension.

An especially advantageous process of that type has been described and claimed in the W. C. Ekholm Patent No. 2,599,981 in accordance with which a violently swirling stream ci' hot blast flame gases is established and maintained in an elongated, unobstructed, heat-insulated reaction `chamber of circular cross-section and the hydrocarbon to be decomposed, herein designated hydrocarbon make, is introduced through the side wall of the furnace chamber and injected radially into the swirling, hot gas stream passing through the chamber.

ri`he present invention relates more particularly to improvements in that type of process just described, which have been found to be especially advantageous in such operations in which a heavy hydrocarbon tar or residue is used as the hydrocarbon make. The invention also includes improved apparatus especially adapted tothe carrying out of the process.

Hydrocarbon tars or residues are extensively used for the production of carbon black because of their ready availability at relatively low costs and their high combined carbon content. Coal tars and highly aromatic residues, obtained, for instance, by thermally cracking recycled stock from the catalytic cracking of petroleum to produce motor fuels and the like, have been widely used for this purpose.

Carbon black is extensively used in the compounding of rubber for producing automobile tires, and the like. It is, or" course, desirable that the rubber composition of automobile tires possess high tensile strength. It is likewise desirable that such compositions possess good rebound characteristics so as to minimize overheating in use. The rubber-compounding characteristics of the carbon black used greatly influence these and other characteristics oi the finished tire.

Unfortunately, it has been found that carbon blacks which impart high tensile strength to such rubber compositions usually do not impart high rebound, and that carbon blacks which impart optimum hysteresis characteristics tothe rubber, as indicated by high rebound, usually have lower tensile strength characteristics.

The present invention provides a method and means whereby carbon blacks embodying both high tensile strength and high rebound characteristics may be economically produced from the heavy, aromatic tars and residues previously described.

The process of the present invention diiers from that of the Ekholm patent, just noted, primarily, inthe reversing of the direction in which the hydrocarbon make is radially injected into the swirling stream of hot blast flame gases, i.e. the hydrocarbon make is injected radially outwardly from the center of the furnace chamber into the hot, swirling gas stream, instead of radially inwardly from the outer periphery of the hot gas stream, and thereby utilizing in a unique manner, and to greater advantage,

the velocities of the swirling hot gas stream and entering make stream.

The present process, accordingly, comprises establishing and maintaining within the cylindrical re-action chamber a stream of hot blast flame gases movinglongitudinally therethrough along a helical path at high velocity, and injecting the liquid hydrocarbon make, as a gasatomized spray, into the hot gas stream from a position at, or in close proximity to., the longitudinal axis of the chamber and directed radially outwardly toward the delineating side wall of the chamber.

As more fully hereinafter described and illustrated, when a helically flowing gas stream is established Within a cylindrical chamber, such as that with which we are here concerned, for instance, by injecting a combustible gaseous mixtureinto the upstream end of the chamber in a direction substantially tangential to the inner circular side wall thereof and burning the mixture therein, we have found that there is a very substantial ditference in linear velocity of the hot gases along their helical path at various zones over a transverse section of the upstream end of the chamber. This velocity has been -found to be relatively slight in a circular zone of substantial diameter coaxially with the longitudinal axis of the chamber. This zone of relative low velocity may have a diameter approximately one-half that of the chamber. But outwardly beyond this central Zone the swirling of the blast gases is greatly intensified, reaching a maximum or peak velocity and again diminishing as the chamber side Wall is approached, as hereinafter illustrated.

In accordance with the present invention, it lis essential that the mass velocity of the hydrocarbon make spray, relative to the mass velocity of the swirling blast flame gases, be such that the spray of make penetrates the hot gas stream to the zone of maximum Velocity before being entirely dispersed. The mass velocity ratio necessary to establish this condition, will vary somewhat with the diameter of the chamber, but may be readily determined by visual observation through the customary peep-holes during operation and necessary adjustments made to establish and maintain this prescribed condition.

The invention will be further described and illustrated with reference to the accompanying drawings of which:

FiG. l represents, somewhat fragmenta-rily and diagrammatically, a longitudinal sectional View of a carbon black furnace of circular cross-section embodying the present invention,

FIG. 2 is a transverse sectional view along the line 2-2 of FIG. 1.

FIG. 3 is a somewhat enlarged longitudinal sectional view of a spray assembly, taken along line 3-3 of FIG. 4, especially adapted to the injecting of the liquid hydrocarbon make, p

FIG. 4 is a transverse sectional View along the line 4-4 of FIG. 3,

FIG. 5 is a transverse sectional of FIG. 3,

FIG. 6 is a transverse sectional View along the line 6 6 of FIG. 3,

FIG. 7 is a perspective View of the convex half of the oil-steam oriiice head of the assembly of FIG. 3,

FIG. 8 is an enlarged longitudinal sectional View of a somewhat different form of spray assembly, which has been used with particular advantage for injecting the liquid hydrocarbon make,

FIG. 9 is a transverse sectional view along line 9--9 of FIG. 8,

FIG. 10 is a graphic illustration of the hydrocarbon make spray pattern formed when using a spray assembly ofthe type shown in FIGS. 3, 4, 5, 6 and 7 of the drawings,

view along the line 5-5 FlG. l1 is a graphic illustration of the variation in` blast gas velocity over the cross-sectional area of a cylindrical reaction zone, 1l inches in diameter, of the type the combustion zone thereto,

EIG. 12V is a graphic illustration of the variation in blast gas velocity over the cross-sectional area of a combustionvzone 42l inchesLD. and. 12l` inches long at a section at its entranceinto an 1l inch LD. reaction zone ofv a furnace such as shown in BIG. l, and

BIG. 13V 'is al graphe illustration ofV the variation in blast gas yelocity over the cross-sectional arca of a cornbustion zoned() inches LD. and l6inches long at a section 4-Y in'ches upstream from the entrance to an lll inch I-D- reaction zone as shown in FlG. 1.

Referring to FIG. `1 ofthe drawings, thereis represented at 1 an elongated cylindrical reaction chamber leading at itsy downstream end into a vertical` cooler, fragmentarily represented at 2, The cylindrical wall 3 of `chamber 1 is of suitable furnace refractory adaptable to withstand the necessary high temperatures and is surrounded by a layerA of tire brick 4i which, in turn, isA surrounded by al layer ofheatfinsulating material S, all encased by metal jacket. 6,.

At its upstream end, the chamber 1 is enlarged to forma combustion Zone` 7 of adiameter substantially in exessof its ,length to provide ay larger volume for the burningof a combustible mixture, of fuel gas and air, for instance, introdncedinto zone 7 through burner ports 8 directedinto zone 7 substantially tangential to the cylindrialfside wall thereof, as more fully shown in FIG. 2.

The enlargement of chamber 1 at its upstream end, as shown at 7, for instance, makes itpossible to increase therate at which the hot blast ame gases are generated and has been generallyI found advantageous. However, it willbe understoodthat the present invention, in its broaderwaspect, is applicable towoperations of the type described carried on inv furnace chambers of substantially uniform diameter throughout.y Further, the particular construction of the furnace,'except as hereinafter prescribed, `rrliay bel varied considerably without departing frolinithescope of this invention. Forinstance, the hot brlastwiilameV gases may be separately generated outside of the' chamber shown, and the4 hot products of combustion, atthe necessary temperatureI to decompose1 the hydrocarbon make, injected tangentially into the chamber. It is essential, however, that there be established and maintained within the furnaceA chamberV aswirling stream of the hot 4blastV -iiarney gasest flowingllongitudinally, through the chamberalong a helical pathfaty high velocity, as pre- VQUSl'Y nted- 'Iheenlarged combustion zone 7 is circular in crosssection and coaxially positioned with respect tovchamber 1" and'isl delineated by walls'of furnace refractory 9. Anannular air chamber. 10 is positioned about the outer wallT ofcombustion zone-7 and is connected thereto by a plurality of burner ports S-proyided with burner tubes 11, cut'diagonally at their outer ends, and through which fuel inlet pipes 12extendcoaxially. Air. for combustion is delivered under pressureA through air `conduit 413.V

yIn`FIG. 'l VtwoV separate sets of tangential burners are shown. It will be understoodthat only. one set of burner ports is usually'required butthat where two are provided, they'vmay be used either interchangeably, depending upon operating conditions required, or both sets yof burner ports may be used simultaneouslywithout departing from the scope of this invention. The fuel pipes 12 are removably supported by caps 14, threaded onto, or otherwise secured to, the projecting tubes 15.

Hydrocarbon make injection assembly 1(` extends coaxially through the upstream furnace wall 17 into the combustion Zone Tand, whereit passes through the furnace wall, is surrounded by a` sleeve 118 through which the assembly is free to slide, so asV to adjust the position of thespray head thereof with respect to the burner ports 8 and with respect to the downstream end wall 19 of the tangentially to vchamber 10V combustion zone. This adjustment may be accomplished by appropriate manipulation of the set screws 2G extending through collar 2l which is secured to the furnace structureby ilanges 22.

This spray assembly will be more fully described with reference to FIG. 3. As there shown, the spray assembly comprises a central, cylindrical passageway 23, delineated by tube wall 24, and surroundedV by a coaxial annular passageway 25 lying'between tube wall 24 and tube wall 26. The annuular passageway 25 is in turn surrounded by coaxial passageway 27v of annular form but divided in halves by partitions 2d, all as more fully shown in FIGS. 3 and 6 of the drawings. The outer end of the assembly is closedby end wall ida.

At the inner end ofthe spray assembly, the passageway 23 flares outwardly rand communicateswith a plurality of radially directed spray ports 2,91, `as more clearly shown.

in FiGS. 4 and 7, these ports beingenlarged at their inner and outerv ends and somewhat restricted at their intermediate portion. The outer ends of these ports. open directly into the furnace chamber through narrow slots,

`advantageously ofya width of the order of 3,@4 oi' an inch,

throughwhich streams ofthe liquid hydrocarbonmake is sprayed radially into the furnace chamber in admixtureV with the atomizing gas, advantageously steam, under pressure.

In operation, the conduit 23 and the spray ports 22 are proteeted from overheating b y passing water, or other cooling medium, into the jacket 27 through inlet 3i), and along one side of the partitions 218, through hollow cap screws 31 into end chamber 32, positionedgat the innermost end of the spray assembly, and outwardly therefrom through corresponding hollow cap screws 31. and passageway 27', on the other side of the partition 28, from which it is discharged through outlet 313.

As appears more clearly from FIG. 3, the inner end of,

the spray assembly comprises a spray head 3d, convex atits upstream end to t nicely against the concave portion 350i the spray assembly and secured thereto by the hollow cap screws 3i, advantageously adjustable, so4 as to vary the longitudinal width of the sprayv ports 29 at their` `outer ends. Beyond the spray head 34 is the end cap 3d secured to head Sdby means of machine screws 37and by yshank 33, extending'outw-ardly from spray head S4- and Hconstituting an integr-al part thereof, and nut 39.

Where the hot blast ame gases are of 'an oxidizing nature, itis frequently desirable to neutralize the oxidizing capacity of the hot blast flame gases before they come into Contact with` the liquid hydrocarbon make, vas more fully describedinllatent 2,782,101. For this purpose, the spray assembly just Adescribedris provided with the annular passageway 25 to which a gaseous fuel, advantageously natural gas, is passed through one or more inlets indicated at ddfand is jetted into the furnace chamber throughradially directed gas ports dll, as shown more clearly in FIGS .,3 'and l5.

The spray iassemblyjust `described is especially adapted to the injection of lliquid hydrocarbon make as separate.

sprays, dispersedin steamA or lOther atomizing gas by wellknown conventional means, not necessary here to describe, andfrom which the dispersion is passed to tube 23 through inlet d2.

The inner portion of thisl spray assembly, wheredeposits are more likely to form, is readily disassembled for cleaning by removing nut 39, machine screws 37 and hollow cap'serews 3l. The remaining portions of the assembly maybe fastened-togetheriu any suitable mannen,

advantageously by welding as indicated inthe drawings.

A modified, and somewhat simpliied, spray assembly especially adapted to the injection of the gas-atomized make spray in the forrnof a radially-extending disk, and

which has been used with particular advantage, is represen-ted iatFiGQS. The assembly there shown comprises an outer casing 43 within which there are coaxially pospaanse sitioned four annular chambers 44, 45, 46 and 47. The innermost end of the assembly comprises a scr-ew cap i8 forming the inner walls of a cooling-fluid chamber 49.

In operation, water or other suitable cooling fluid, is passed through tube 50, coaxially extending through annular chamber 47, into cooling chamber 49 from which it passes outwardly through openings 5i, extending through spnay head 52, through the annular cooling jacket dfi, from which it passes through one or more exit tubes 53.

The liquid hydrocarbon make, dispersed in steam or other atomizing gas as previously described, is introduced under pressure through one or more inlet tubes and passes through the annular chamber '46 into the enlarged chamber 55 within the spray head 52. From chamber 55, the steam-oil mixture passes under pressure through ports 56 into the annular chamber S7 from which it passes through the radially-extending slot 5S into the furnace chamber, the annular chamber 57 and slot 58 being shown on Ia somewhat enlarged scale Within ycircle 5'9 of FIG. 8, for clarity.

The Width of the slot 58 may be varied by adjustment of cap dit, -for instance by turning cap 4S with respect to head S2 to which it is secured by threads indicated at 60, shims being used to insure la tight closure, where necessary.

The `annular chambers shown at and 47 may be dead-air spaces and Vented through end plate 61 through vents indicated at 62 to avoid excessive pressure build-up. Where it is desired to use auxiliary gas, as described with respect to FIG. 3, the spray head of FIG. 8 may be modified as indicated in dotted lines whereby natural gas or the like is charged through gas inlet 63 into the annular chamber 45 and passes therefrom into the furnace chamber through the radially projecting orifices 64. When so modified, the vents 62 leading from chamber 45 will, of

course, be closed.

Should it become necessary to clean the assembly just described, it is only necessary to remove cap 43 in order to obtain access to all portions of the nozzle assembly where deposits would be apt to accumulate. The remain ing elements of the assembly may be permanently fastened together in any suitable manner, for instance by welding, as indicated in the drawing.

In carrying out the process of the present invention, a combustible mixture, advantageously a gaseous `fuel and air, may be injected tangentially into combustion zone 7 through the burner ports 8 and burned -as it enters the chamber to `form a swirling stream of hot blast iiame gases passing longitudinally through the chamber along a helical path at high velocity. As previously noted herein, we have found that under such conditions the linear velocity of these blast liame gases varies materially over the crosssectional area of the furnace chamber. This velocity variation is illustrated in FIGS. 11, 12 and 13 of the drawings in which the gas velocity, in feet per second, is plotted against distance, in inches, `from the chamber wall.

FIG. 1l illustrates this velocity variation at a section just downstream from the entrance of the swirling gas stream from the enlarged combustion zone into an ll-inch LD. reaction chamber of a furnace of the type shown in FIG. l. From this graph, it appears that the linear velocity of the swirling gases in a coaxial zone at the center of the chamber is only about 200 `feet per second while in the zone approximately 2 inches inwardly from the chamber wall the velocity is in excess of 800 feet per second. At even less distances from the chamber wall, there is a material drop in linear velocity of the swirling gases, but even here the gas velocity is substantially in excess of that in the vicinity of the axis of the chamber. Further, it will be noted from this graph that the velocity drops sharply on either side of the peak velocity prevailing in a zone extending inwardly from the furnace wall a distance of about 1/6 to about 1/3 the chamber radius.

FIG. 12 represents this velocity variation in a furnace of the type shown in FIG. 1 having a reaction chamber 1l inches in diameter preceded by an enlarged combustion zone 42 inches I.D. and 12 inches long at a section at the extreme downstream end of the combustion Zone. At this point, the central core of relatively' low velocity is approximately 5 inches in diameter, and just to the outside of the core the velocity rises sharply from about 200 feet per second to a peak of 9G() feet per second and again dropped oti sharply in the direction of the outer wall.

FiG. 13 illustrates this condition in a similar `furnace having an enlarged combustion zone 3G inches I D. and 16 inches long at a section 4 inches upstream `from the entrance to the 1l inch I.D. reaction chamber. It will be noted that the pattern is very similar to that of FIG. l2.

While the data on which these graphs are based may not he entirely accurate, they were arrived at by accepted engineering methods and serve to illustrate the manner in which the gas velocity varies relatively over the diameters of various sections of the furnace chamber.

As shown by these graphs ,the position of this Zone of peak velocity has been found to vary somewhat with the diameter of the particular furnace chamber and the particular section thereof. It will also vary somewhat with the initial inlet velocity of the tangentially injected combustible mixture or hot blast flame gases. But for any operation, this zone of peak velocity is readily determinable by conventional gas-velocity-measuring equipment and when plotted-against distances from the chamber wall, as in FIGS. l1, 12 and 13, the curve will be found to conform generally to those shown.

We have found that we can utilize to great advantage this difference in linear velocity of the hot blast flame gases to control the characteristics of the resultant carbon black and to minimize the difficulties heretofore experienced in operations in which a gas-atomized residual hydrocarbon or tar is radially injected into the swirling blast gas stream.

One such difficulty is believed to be due to the presence of substantial amounts of thermally stable colloidal` bituments, or other carbonaceous or coky materials, in these heavy hydrocarbon residues. While we do not intend to be bound to any such theory, it is our present belief that these coke-like particles and colloidal bitumens are, in conventional practice, carried through the furnace chamber and are thereafter collected with the carbon black, deleteriously affecting the rubber compounding characteristics of the black, and that in accordance with our present invention these thermally stable colloidal bitumens and the like, injected into the furnace chamber with the make, are quickly separated from the desirable carbon black-forming hydrocarbons, as the make is injected into the hot gas stream, by being thrown by centrifugal forces, or otherwise, against the furnace wall and there burned.

But regardless of theory, we have found that the previously described marked improvement in the resultant canbon black is obtained in accordance with our present inventon by injecting the liquid hydrocarbon spray radially outwardly from the zone of minimum gas velocity into the zone of maximum gas velocity. Within the zone of minimum blast gas velocity, the mass velocity of the hot Iblast gases is, of course, at a minimum. On the other hand, the radial velocity of the liquid hydrocarbon make syrays is at a maximum at the point of injection and consequently the mass velocity of the spray streams is at a maximum. Therefore, the entering liquid spray is not immediately shattered and dispersed by the hot blast iiame gases, as in the process of the Ekholm Patent 2,599,- 981, nor is there formed a central core of concentrated hydrocarbon as previously proposed by injecting the hydrocarbon make axially into the chamber.

In accordance with the present invention, the injected `hydrocarbon spray passes substantially radially outwardly,

.by reason of its relative high mass velocity, until it approaches the maximum blast gas velocity zone. The spray is then struck by the extremely high velocity blast subject to considerable variation.

- downstream end walls of that zone.

ame gases and the hydrocarbon thereby subjected to tremendous shearing action and centrifugal forces. It is believedthat fby reason of these centrifugal forces and the :initial high velocity of the make spray the coke-like and other solid particles present in the hydrocarbon make are thrown outwardly into the zone of diminishing velocity adjacent the chamber wall and the there consumed, probably aided 'by :catalytic action ofthe chamber Wall.

A diagrammatic representation of the pattern of the liquid hydro-carbon make spray injected as separate streams by means of an atomizing spray assembly, such as represented at FIG. 3 of the drawing, is shown in FlG. 10. A somewhat similar pattern is formed when a continuous radial disk spray of the hydrocarbon make is injected into the furnace chamber, as by means of the spray assembly shown in FlG. 8.

The longitudinal position of theyradial make spray is ln a furnace of the type shown, it may be positioned either in the enlarged combustion'zone, advantageously in the downstream half thereof, or -in the upstream end of the reaction chamber of reduced diameter. The optimum position will depend to some extent upon the desired properties of the resultant carbon black.

Vle have found, for instance, that in a furnace of the type shown in the drawings having a combustion Zone of 33 inches LD. and 2l inches long and a downstream section l1 inches LD., the spray position may be varied over a Zone ranging from 2 inches to 6 inches upstream from the entranceto the reduced section, other condiA tions remaining constant, without material changes in the property of the carbon black. However, when moved to a position within the range of 8 inches to 10 inches upstream from the entrance to the reduced section, the resultant black has been found to change from an ISAF grade to an HAF grade. Where the spray is moved to a position within the combustion zone less than 2 inches upstream from t'ne entrance to the reduced section, a somewhat finer product has resulted.

In a similar furnace having a combustion zone 30 inches IJ). and 16 inches long, we have, with advantage, operated with the make spray positioned in the enlarged combustion zone 4 inches upstream from the reduced section for producing an ISAF grade black of high quality- The initial velocity of the make spray, partly vaporized by the atomizing stream, at the point of discharge from the spray nozzle, is of the order of 1600 to 3200 feet per second,l and nonvaporizable portions of the oil will be injected into the furnace at substantially those velocities. But these unvaporizable portions of the oil, previously referred to as colloidal bitumens, have a specic gravity ranging from 1.06 to 1.21, weighing between 66 and 76 pounds per cubic foot, whereas blast llame gases at operating temperatures weigh about 0.015 pound per cubic foot. Thus the mass velocity of these unvaporizedrportions of the make exceeds that of the blast gases by a factor approximating 800011 and, therefore, they are not diverted from their radial path.

The invention and the effectiveness thereof will be further illustrated by the following specific examples.

EXAMPLE I These operations were carried out in a carbon black furnace, such as illustrated in FIGS. l and 2 of the drawings, of which the longitudinal dimension of the enlarged combustion Zone was 16 inches, the diameter thereof was 30 inches, the smaller diameter of the reaction chamber was 11 inches and the longitudinal dimension of that portion of the chamber was about 11 feet. The furnace was provided with two sets of tangential blast burners of six burners each symmetrically positioned about the chamber, the respective sets of burners entering the combustion zone about 31/2 inches from the upstream and These burner ports were 3 inches inside diameter. ports were in operation.

In a furnace of thistype and ofthe stateddirnensionsA it has 4been found especially advantageous tov adjust the spray longitudinally to a position not less than four inches nor more than seven inches upstream from the downstream end-wall of the enlarged combustion zone, and in the following Vrun A, made in accordance withthe present invention, the spray was positioned 4 inches from said wall.

in each ot these operations, the hydrocarbon make was a highly aromatic residual oil of the type currently used in the production of carbon black. Fuel gas, consisting of natural gas, was charged to the furnace ata total rate In these runs all burner of 15 ,400 cubic feet per hour andfair for combustion was charged at a rate of 180,000 cubic feet per hour.

ln operation A, carried on in accordance with the present invention, the hydrocarbon make, dispersed by steam at a pressure of 75 lbs. per sq. in., was charged at a rate of 155 gallons per hour through a spray assembly of the type illustrated in FlG. 3v adaptedk to inject 12 symmetrically positioned spray streams radially outwardly into the swirling stream of hot blast'fiame gases. The spray head of this assembly was approximately 21/2l inches in diameter.

ln run B, here shown for the purpose of comparison, the operating conditions weresubstantially identical withv those just described except that the hydrocarbon malte was directed radially inwardly into the swirling -blast llame gas streamv as described in the previously noted Patent No. 2,599,981.

The colloidal and chemical characteristics of theV carbon black resulting from the respective runs are set` forth in the following tabulation:

When the` respective carbon blacks were compounded with natural rubber, in accordance with identical formulations, and the resultant rubberk compositions cured and tested by standard procedure, the followingvalues were,`

F'! 0J obtained:

T cible vIl Run A- B Cured at 275 F. for 35 Minutes:

L-BOO 1, 360 1,260

3,130 2, 8704 4, 53()y 4,360. 670y 68()` Shore Hardness 53 51 6, Cured at 275 F. for 70 Minutes:

d L-ano 1,875 1. 62o 3, 875 3, 450 Ten 11e 4, 700 4, 540 Percent Elongation. 605 640A Shore Hardness 57 57 Percent Rebound 67. 8 66.' 2 Electrical Resistivity, Log R.. 2. 7 3.0. G5, Maximum Tensile 4, 700 4, 550

EXAMPLE II In a further series of runs in a furnace of vsubstantially the same `dimensions as that used in the preceding run A,

air was charged at the rate of 158,000'cubic feet per hour, the ainfuel gas ratio was 12.2:1l and a heavy aromatic hydrocarbon make, such as used in run A, was charged at the rate of 174 gallons per hour. The oil was preheated to thetemperature of 400 F. and the atomizing gas was steamed at a pressure of 80 pounds per square inch. In run C, the radially-directed spray was positioned 4 inches upstream from the entrance to the reduced section of the furnace chamber. In run D, the spray `was positioned flush With the downstream end wall of the enlarged combustion zone, and in run E the spray was positioned within the reduced section of the furnace chamber 4 inches downstream from the entrance thereto.

The characteristics of the resultant carbon lblacks and their rubber compounding `chracteristics in synthetic rubber are set forth in the following tabulation:

Table III Run C D E Color, ABC 139 141 141 Tinting Strength, Percent Standard. 115 119 116 Oil Absorption, Gallons per 100 lbs 14. 9 15.4 15. 4 Iodine Absorption 72 69 72 DPG Absorption 5. 41 5.06 5. 78 Rubber Properties:

Cure Time, minutes. 40 37 35 L-300 l, 360 l, 435 1, 450 Tensile Strength... 3,525 3, 650 3, 625 Percent Elongation 615 626 610 Shore Hardness 55 56 57 Log R Elec. Resistivity-- 3. 5 3. 7 8. 5 Percent Rebound.. 50.6 50. 6 50. 6 Abrasion Resistanc 94 91 D5 Maximum Tensile. 3, 575 3, 700 3, 650

The foregoing rubber compounding characteristics were determined by `conventional methods yon identically prepared compositions of LTP-14 (low temperature polymer) synthetic rubber in` which the respective canbon black products were incorporated.

EXAMPLE III Y Afurther series of runs was carried out in a furnace such as used in run A of Example I except that the enlarged combustion zone ywas 33 inches I D. and 21 inches deep. In these runs, air was charged to the furnace at the rate of 160,000 cubic feet per hour, the air-fuel gas ratio was 12.4;-1 and the hydrocarbon make was a heavy aromatic hydrocarbon residue and was charged to the furnace at the rate of 168 gallons per hour. In these runs F, G, H and I, the radial spray was positioned 4 inches, 6 inches, 8 inches and l0 inches, respectively, upstream from the entrance to the reduced section of the furnace chamber. The characteristics of the resultant carbon blacks so produced are set forth in the following tabulation:

Table l V Run F G H I ABC Color 139 137 134 133 Tinting Strength, percent Standard 123 122 116 113 Oil Absorption, Gallons per 100 lbs 18. 2 16. 9 16. 0 17. 0

10 in many instances, has been found desirable. Such high oil load operation is illustrated by the following examples:

In this run made in accordance with our improved method, the apparat-us used was identical with that used in run A of Example I. Air was charged to the furnace at the increased rate of 234,000 cubic feet per hour, the air:fuel gas ratio was 12.3:1 and tne hydrocarbon make, identical with that used in run A, was charged to the furnace at a rate of 210 gallons per hour. The radial spray was positioned 4 inches upstream from the entrance to the reduced section of the furnace chamber.

The characteristics of the resultant carbon black, and its rulbber compounding characteristics in natural rubber, are set forth in the following tabulation under column I. For comparative purposes, there are set forth ill column K of the tabulation the 'characteristics of a high-grade commercial ISAF carbon black, not made by our process but of approximately the same surface area, as determined by the electron microscope.

Here, also, a substantial improvement in both tensile strength, percent rebound, and road wear characteristics are shown.

In determining the rubber compounding characteristics of the carbon blacks of Examples I and IV in natural rubber, the following formulation was used:

Parts Natural rubber smoked sheets Carbon lblack 45 Sulfur 2.75 Zinc oxide 3 Pine tar 3 Stearic acid 3 Agerite HP l NOBS Special 0.35

In determining the rubber compounding characteristics of the carbon blacks of Example II in synthetic rubber, the following formulation was used:

Parts LTP (low temperature polymer) 100 Carbon black 50 Zinc oxide 3 Stearic acid beads 3 Paraux 9 B-L-E 1 Sulfur 1.6` Altax 0.6 DPG 0.75

In the foregoing tabulations, Paraflux is a trade name for an asphaltic iiux product used as a plasticizer; B-L-E is a trade name for a diphenylarnine-acetone reaction product used as an antioxidant; Altax is a trade name for benzothiazyl disulfide used as an accelerator; Agerite HP is a trade name 4for phenyl-beta-napthylamine plus diphenylparaphenylene-diamine used as an antioxidant; and NOBS Special is a trade name for N-oxydiethylenebenzothiazole-Z-sulfenarnide used as a delayed action accelerator.

Atypical analysis of theV heavy aromatic hydrocarbon residueV used in the foregoing examples'isas follows:

Viscosity, SSU at 210` F. 47 Indexof refraction 1.645 A.P.I. gravity 1.8 Percent Ramsbottom carbon residue 8.98 Molecular weight 264 Itv will be understood,` however, that the utility of this invention is not restrictedto this particular type of liquid hydrocarbon but, in its broader aspect, also contemplates the use ofv hydrocarbon distillate oils andother hydrocarbon residues or tars'. Asv previously noted herein, the invention is especially applicable to the use of hydrocarbons of the residuum type containing colloidal bitumens or the like.

We claim:

l. In they process forproducing carbon black by the decomposition of hydrocarbons in which there is established and maintained withiny an elongated, heat-insulated reaction chamber of circular cross-section, a'swirling stream of hot blast arne gasesr passing longitudinally through the chamber alongV a helical path at high velocity, the axialgcore of said gas stream swirling at a relatively low velocityrand the gas velocity reaching a maximum in an annular zone intermediate said core and the periphery oflthe chamber, and the hydrocarbon to be decomposed isseparately and forcefully injected radially into said het gas stream and is dispersed therein and decomposed by heat absorbed therefrom to form carbon black in suspension, the etiiuent passing from the downstream end of the chamber and the carbon black separated and collected, the improvement comprising the step of injecting the hydrocarbon to be decomposed'into the hot gas stream as a gas-atomized spray of liquidi hydrocarbon initiated adjacent the longitudinal axis ot the chamber and directed radially outwardly'toward the delineating side wall of the chamberv at an initial linear velocitysuch that the spray penetrates the swirling stream of hot gases to the zone of maximum velocity ofsaid gases 2. The process of claiml in which the'hydrocarbon to be decomposed'is a high molecular weight, highly aromatic tarry residuum.

3. The process of'claim 1 in which the atomizing gas is steam.

4; In the process for producing carbon black by the decomposition of hydrocarbons in vwhich a combustible mixture off a hydrocarbon fuel `and an oxygen-containing gas is blasted tangentially into a cylindrical combustion zone of an elongated heat-insulated reaction chamber, saidv combustion zone having a diameter greaterY than its length land, opening. at its downstream end into a coaxially positioned reaction` Zone' of saidchamber of smaller diameter and of a lengthr greater thanits diameter, and thef combustible mixture is burned in the combustion zone to=forma swirlingstreanr of hot blastame gaseslowinglongitudinally through .said chamberatalhigh"v velocity alonga.helical,path,.,the..axialV core ofsaid gas stream swirlingat relatively low velocity and the gas velocity reaching a. maximum in an annular. zone intermediate said ooreand theperiphery ofthe. chamber, and the hydrocarbon to vbedecomposed is. separately and forcefully injected radially into said hottgasstream and .is dispersed therein Vand decomposedbyheat. absorbed thereform to form carbon black in suspension, the eluent passing from the downstream endofl the chamben and theearbonrblacky separated and collected,.the improvement comprising the step of injecting the hydroearbont'ol be decomposed into` the hot gas stream as a gas-at'omizedA spray of' liquidf hydrocarbon'initiated adjacent the longitudinal axis .of the chamber and directed radially outwardly towardthe delineating side wally of the chamber at anV initial linear velocity such that the spray penetrates-the swirling stream of hot gases to the zone ofI maximum velocity of saidgases.

5. The processof claim 4 in` Whiclfvthe radial-.spray of' the liquid hydrocarbon is positioned in the reaction zone of the furnace chamber adjacent theupstream endjthereof.

6. The process ot claim 4in which'the radiali spray-of` the liquid hydrocarbon is positioned within the down#- stream halt of the enlarged combustion zone.

7. The process of claim-1 in which the hydrocarbon tobe decomposed contains colloidalbitumensandthe initial linear velocity of the radial spray. is such that the` mass velocity of said bitumen particles exceeds the maximum massveloci-ty-'of the hot blast arne gases.

8. Apparatus for producing carbon black comprising an elongated, heat-insulated lfurnace chamber of circularA cross-section' and having at its upstreamV end a combustion section of greater diameter than its length which opens at its downstream end into -aV coaxially positioned elongated reaction section of reduced diameter, a plurality of burner ports extending 4through the'wall ofthe chamber and directed tangentially into said combustion section, means for introducing a combustible gaseous mixture therethrough into the combustion section, a hydrocarbon oil spray assembly comprising an outer cylindrical casing extending coaxially through theupstrearn end wall of thel chamber, an oil chamber positioned in the downstream endof the casing, a conduit extending through the casing Vthat the constricted; radially-directed passageway extends' uninterruptedly about the periphery of thercasing, where'- by a gas-atomized" spray of thev oil in the form ofl a' radially-directed disk is kinjected into the furnace chamber;

l0.` The apparatus of claim 8` further characterized in thatv the constrictedM radially-directed passageway comprises a multiplicity of radially-directedorifices uniformly positioned about the periphery of the casing.

References Cited-inthe le of'thispatent UNITED STATES PATENTSA 1,874,002 Fantz Aug; 30, 1932V 2,368,827 Hanson et al Feb. 6, 1945V 2,408,282 wolf Sept. 24, `1946 2,809,098 Larson Oct. 8, 1957 2,825,633 Steele Mar. 4, 1958 2,864,673 Mannini Dee. 16, 1958 

1. IN THE PROCESS FOR PRODUCING CARBON BLACK BY THE DECOMPOSITION OF HYDROCARBONS IN WHICH THERE IS ESTABLISHED AND MAINTAINED WITHIN AN ELONGATED, HEAT-INSULATED REACTION CHAMBER OF CIRCULAR CROSS-SECTION, A SWIRLING STREAM OF HOT BLAST FLAME GASES PASSING LONGITUDINALLY THROUGH THE CHAMBER ALONG A HELICAL PATH AT HIGH VELOCITY, THE AXIAL CORE OF SAID GAS STREAM SWIRLING AT A RELATIVELY LOW VELOCITY AND THE GAS VELOCITY REACHING A MAXIMUM IN AN ANNULAR ZONE INTERMEDIATE SAID CORE AND THE PERIPHERY OF THE CHAMBER, AND THE HYDROCARBON TO BE DECOMPOSED IS SEPARATELY AND FORCEFULLY INJECTED RADIALLY INTO SAID HOT GAS STREAM AND IS DISPERSED THEREIN AND DECOMPOSED BY HEAT ABSORBED THEREFROM TO FORM CARBON BLACK IN SUSPENSION, THE EFFLUENT PASSING FROM TH DOWNSTREAM END OF THE CHAMBER AND THE CARBON BLACK SEPARATED AND COLLECTED, THE IMPROVEMENT COMPRISING THE STEP OF INJECTING THE HYDROCARBON TO BE DECOMPOSED INTO THE HOT GAS STREAM AS A GAS-ATOMIZED SPRAY OF LIQUID HYDROCARBON INITIATED ADJACENT THE LONGITUDINAL AXIS OF THE CHAMBER AND DIRECTED RADIALLY OUTWARDLY TOWARD THE DELINEATING SIDE WALL OF THE CHAMBER AT AN INITIALY LINEAR VELOCITY SUCH THAT THE SPRAY PENETRATES THE SWIRLING STREAM OF HOT GASES TO THE ZONE OF MAXIMUM VELOCITY OF SAID GASES. 